Solution Mining and a Crystallizer for Use Therein

ABSTRACT

In solution mining, holes are drilled parallel to the ground in the ore body to form a series of zigzag channels. These holes are connected to respective holes from the surface to provide a feed and delivery path and a solvent is circulated through the system so as to dissolve the ore and carry the ore to the surface. The flow of the solvent through the holes forms circular caverns at the intersection of the horizontal hole as well as meanders by eroding the holes so as to gradually extract the ore on each side of the hole. At the surface the ore is extracted in a series of crystallizers each formed by a vessel with an exterior cooling system and an internal wiping system providing shear inside the vessel. The solvent is topped up, reheated and returned to the paths to continue the process.

This application claims the benefit of priority under 35 U.S.C. 119 of Provisional Application Ser. No. 61/296,731 filed Jan. 20, 2010.

This invention relates to a method of solution mining and to a crystallizer for use in solution mining.

BACKGROUND OF THE INVENTION

In-situ leaching (ISL), also called in-situ recovery (ISR) or solution mining, is a process of recovering minerals such as copper and uranium through boreholes drilled into the deposit. The process initially involves drilling of holes into the ore deposit. Explosive or hydraulic fracturing may be used to create open pathways in the deposit for solution to penetrate. Leaching solution is pumped into the deposit where it makes contact with the ore. The solution bearing the dissolved ore content is then pumped to the surface and processed. This process allows the extraction of metals and salts from an ore body without the need for conventional mining involving drill-and-blast, open-cut or underground mining.

Conventional solution mines create individual caverns, usually by dissolving salt from beneath the ore body, then rubblizing the ore into the cavern and dissolving the ore in fresh water or dilute brines to form near saturated solutions at temperatures equal to ore temperature (or slightly higher). Caverns tend to develop vertically and, in some cases, consideration has been given to connecting caverns.

In order to collect the ore from the solution, crystallization systems are necessary at the surface.

Conventional solution mining systems have difficulty raising the mine temperature above the formation temperature, as well as obtaining fully saturated brines. Thus at the surface they raise the potash concentration and temperature in evaporators. This is the most expensive part of the plant using large amounts of expensive and exotic metals. Large amounts of steam are also required in this process.

The hot concentrated brines are then crystallized in evaporative crystallizers. These are limited to cooling to about 25 degrees C. One mine uses a system which takes the cooled brine to ponds, and make use of natural cold crystallization in open ponds to add to plant recovery. This is still an expensive process requiring careful management and expensive dredging equipment. It also is seasonal with no potential to recover any heat.

SUMMARY OF THE INVENTION

It is one object of the invention to provide an improved solution mining system.

According to one aspect of the invention there is provided a identifying an ore body or bodies at a position below ground;

drilling at least one hole from the surface downwardly to an ore body;

drilling a hole in a direction generally parallel to the ground to interconnected portions of the ore body to form a series of channels extending through the body;

the holes from the surface being connected to two ends of the interconnected portions to provide a feed path to and a delivery path from the series of channels; and

circulating a solvent through the feed path, the series of channels and the delivery path so as to dissolve the ore and carry the ore to the surface through the delivery channel.

Thus the system uses one hole from the surface to the horizontally drilled holes as a feed path for injecting the solvent and acts with one or more vertical holes forming production wells with more than one used if needed for high flow.

The methods described herein are primarily developed for mining of potash but can be used with any other materials for which solution mining is a practical technique including uranium, soda ash and bitumen extraction from tar sands.

The plan is for a simplified method of solution mining which can be used for example in a potash mine, using a novel solution mining plan. The potash plant may include a unique crystallization system, which is termed hereinafter the externally circulated wiped surface crystalliser (ECWSC).

The process described herein is designed to produce saturated or near saturated brines from the mine at a high temperature, at or above the rock temperature at the level of the ore body.

The saturated brine can simply be cooled to produce product in a simplified crystallizer plant with the barren brine from the crystallisers reheated and returned to the mine to further dissolve potash out of the ore body.

This eliminates the need for expensive evaporation equipment and the high operating cost associated with this equipment. Small amounts of water are added to the heated brine to create the amount of brine needed to replace the dissolved ore in the mined area. This results in the dissolution of about 10% of the salt in the mined area.

The mine plan allows the deposition of the salt liberated from the ore (as the potash dissolves) in the mined out area, so only minimal amounts of salt ever are brought to surface.

Brine temperature of the saturated brine can be set by adjusting the input brine temperature. This can not be done in conventional systems, or at best is very limited. The system can be used on shallow deposits with low rock temperature as well as deeper deposits (currently the only candidates for solution mining).

The process described herein is essentially the opposite of the conventional system by setting up circulation first, with caverns developed on a horizontal plane from the established circulation. The approach is to develop the mine from horizontally drilled holes interconnected to form a labyrinth with brine returning to the surface in a vertical production well. The holes are drilled vertically to the ore layer, then horizontally through the high grade ore zone near the bottom of the selected mine zone. Caverns develop at the intersection of the holes as the flow is concentrated around the periphery of the cavern. (Salt is deposited in the inside of the curve). As needed, additional holes are drilled developing the mine field.

In addition meanders will develop in the straight bore of the horizontal portion of the well with a sinusoidal flow pattern developing. Potash will be dissolved following the sine curve with salt deposited on the inside of the curve. The pattern is similar to the pattern formed by the meandering of a stream.

The combination of the intersection and meander development creates an undercut of the ore body, with a circular cross section, (typically about 1 meter diameter but dependant on fluid flow rate and ore characteristics) at the periphery and a thin zone of low flow dissolution over the salt deposit. This slow dissolution zone extends the cavern vertically over time to dissolve out the entire ore zone.

The circulation patterns should extend over time to remove the majority of the ore within the pattern with the vertical dissolution in the low flow area removing the vertical extent of the ore body.

It is an important advantage that all the mine development remains under continual flow throughout the life of the mine. This also simplifies the surface piping since the production well (wells) can be located close to the plant, reducing pipeline cost and reducing concerns about crystallization of the saturated brines on the inside surface of production pipelines.

A saturated brine from a properly designed and operated solution mine can be converted to a final product in a simple plant. Product is recovered from the brine by cooling the brine. Conventional vacuum crystallizers can be used but are limited to cooling to about 25 degrees C. A combination of vacuum crystallizers plus suitable contact cooled crystallisers, or contact cooled crystallizers alone can be used to advantage especially in Northern climates with natural cold available through part of the year to provide cooling media as low as −4 degrees C.

According to another aspect of the invention there is provided a method of solution mining comprising:

identifying an ore body or bodies at a position below ground;

generating a feed path through the ore body or bodies;

circulating a solvent through the feed path, the series of channels and the delivery path so as to carry the ore to the surface through the delivery channel.

wherein the material exiting through the delivery path is cooled to produce product in a simplified crystallizer plant with the barren brine from the crystallisers reheated and returned to the mine to dissolve material out of the ore body;

and wherein a crystallization system is provided for large scale low temperature crystallization applications where high heat exchange is provided through cooling patterns and shear inside the vessel.

The system provides an improved crystallization system for large scale low temperature crystallization applications. The units are simple in design providing high heat exchange through the use of specially designed cooling patterns and shear inside the vessel with wipers continually wiping the inner surface. Crystal growth is enhanced by direct contact of the supersaturated brine with the growing crystal.

The present system is based on the realization that the solubility of potash in a saturated salt solution is dependant, almost linearly on temperature. Typically in the industry, this is used to advantage in crystallizer circuits, by dissolving ore or dust in brines at about 90 to 95 degrees C., then cooling the brines with vacuum to 25 to 30 degrees to precipitate the potash. The temperature difference is about 60 degrees C. Almost identical amounts of potash can be dissolved and recovered in 60 degree brine when cooled to 0 degrees. The same amount of heat is used, and product produced, by operating using 33% more brine at 60 degrees and cooling to 20 degrees.

The big advantage of operating at lower temperature is the availability of low grade heat from the earth, or from other parts of the plant operation. Heat losses are also lower to well strings, etc.

Saturated brines from the mine at 60 to 80 degrees C. (even as low as 30 to 40 if needed) are near full saturation. These brines are fed to the first of a series of the above ECWSC units, cooled by about 10 to 15 degrees, producing high purity potash crystals. The partially cooled brine flows forward to the next unit, in a series of up to 5 units. Final brine temperature is typically 0 to 20 degrees C. Crystal passes forward through the series and finally is pumped forward to a centrifuge and dryer. Larger installations may use several parallel lines of crystallizers.

Cool barren brine from the crystallizers is reheated in heat exchangers, using warmed cooling media, recovered heat from the process and steam or hot water from a fuel fired boiler.

The externally circulated wiped surface crystallizer used herein is a significant further development of the scraped surface crystallizers that have been used in the sodium sulphate industry. These crystallizers have the significant advantage of being able to cool to as low as 0 degrees C., or even lower when supplied with a suitable coolant. In addition they are simple to operate, inexpensive, and allow recovery of most of the heat.

Cooling media, as low as 0 degrees C. or lower can be supplied in winter months (in Canada) from an air-cooled heat exchanger, or a small brine pond. Summer operation is generally limited to 16 to 25 degrees C. using a pond or a cooling tower. Some refrigeration can be used in the summer months with the amount of refrigeration being selected based on cost to balance the added pumping costs of increased flow rates to the mine.

A wiper system includes a series of wiper blades which wipe around the inside surface of the conical drum.

Liquid taken from the top is re-circulated back to the bottom collecting hopper so as to generate a suspension of crystals in the body of liquid gradually moving upwardly in the conical drum. The crystals thus form in the body of liquid and tend to grow rather than create new small nuclei. As the crystals grow and become heavier they tend to collect and settle at the bottom to enter the bottom hopper to be tapped off continually or periodically.

The design supports the recovery of heat by the cooled mother liquor, by using it as a cooling medium from the warmer crystallizers.

The design of the crystallizers uses high flow rates in the ducts or channels in the cooling jacket to get high heat exchange rates. High flow rate is obtained by selecting the right number and rotation of wipers on the interior surface of the heat exchange area. With proper selection of conditions, there is no build-up of crystal in the crystallizer so that the crystal settles to the bottom discharge hopper for collection.

An external circulation leg pumping the return liquid to the bottom maintains the crystal in suspension and incorporates the fresh feed into the suspension.

The arrangement shown herein has the potential to improve crystal growth over other crystallizer systems. The unique design of these crystallizers provides for the development of supersaturated brines and the coarsest crystal bed. This reduces or eliminates the need for subsequent compaction of the crystal mass harvested, if coarse crystal can be grown sufficiently through the crystallization process.

A saturated brine from a properly designed and operated solution mine can be converted to a final product in a simple plant. Product is recovered from the brine by cooling the brine. Conventional vacuum crystallizers can be used but are limited to cooling to about 25 degrees C. A combination of vacuum crystallizers plus suitable contact cooled crystallisers as shown herein, or contact cooled crystallizers alone can be used to advantage especially in Northern climates with natural cold available through part of the year to provide cooling media as low as −4 degrees C.

The system described herein is an improved crystallization system for large scale low temperature crystallization applications. The units are simple in design providing high heat exchange through the use of specially designed cooling patterns and shear inside the vessel with wipers continually wiping the inner surface. Crystal growth is enhanced by direct contact of the supersaturated brine with the growing crystal.

While we describe the process for potash mining, the solution mining technique is expected to find application in bitumen extraction from tar sands using organic solvents, emulsifying agents in water and/or organic solvent base or hot water. Sand may be left in the deposit in whole or in part, or alternately brought to surface for separation and returned to the deposit in whole or in part in the barren feed to the mine.

The mining method may also be used in the extraction of other soluble minerals including soda ash, salt etc.

A special application would be removal of high grade uranium such as found at Cigar Lake. The network of horizontal holes could be used as described for the potash application, though on a tighter pattern, along with acid or carbonate extraction solutions (well known in uranium mining) to remove the ore. High flow rates may be used in the cavern flow to erode the uranium ore. Clays and sand will either remain in the cavern created, or brought to surface, separated from the leachate, with the coarsest material returned to the cavern network to backfill the mined area. Coarse sand in the circulation can be used to enhance the erosion of the relatively hard uranium ore.

The process described herein may offer one or more of the following advantages:

1. Low capital cost (about 1/10 of a conventional potash operation).

2. No solid tailings.

3. Lower energy cost than existing solution mines.

4. Can be developed as a small operation and be viable.

5. Small footprint.

6. Low operating cost (About an 80% reduction).

7. High potash recovery from a small mine area (2,000,000 to 10,000,000 tonnes/square mile).

8. Low carbon footprint. Virtually no chemicals used in the process, except small amounts of chemicals for boiler feed water etc.

9. Less energy than any existing potash mine.

10. Short time from start of construction to full production.

The horizontal drilling in a potash application might be directed by continuous monitoring of gamma radiation as is done in certain oil drilling applications. Potash has a natural K40 isotope producing a gamma radiation. The horizontal portion of the hole will normally not be cased.

One advantage of the system is the possibility of locating the production well or wells near the plant as a permanent installation. This reduces surface pipe cost. Two parallel holes or pipelines will be needed for the feed lines to the wells. Overall the surface disruption to agriculture etc is minimal. The fact that there are no salt tailings is hugely significant in a potash mining operation.

BRIEF DESCRIPTION OF THE DRAWINGS

One embodiment of the invention will now be described in conjunction with the accompanying drawings in which:

FIG. 1 is a schematic illustration of a conventional solvent mining system.

FIG. 2 is a schematic illustration of a solvent mining system according to the present invention showing a series of horizontal connecting bores and showing the cavern development over time caused by the brine flow through the bores.

FIG. 3 is a similar schematic illustration of a solvent mining system according to the present invention showing the horizontal connecting bores and the vertical production hole or well.

FIG. 4 is a schematic illustration similar to FIG. 3 showing the development of meanders or caverns over time caused by the brine flow through the bores.

FIG. 5 is a schematic cross section of an intersection cavern

FIG. 6 is a schematic layout of an above ground crystallization extraction system according to the present invention.

FIG. 7 is a vertical cross sectional view of one of the crystallization components of FIG. 6.

FIG. 7A is a vertical cross sectional view taken along the lines 7A-7A of FIG. 7.

In the drawings like characters of reference indicate corresponding parts in the different figures.

DETAILED DESCRIPTION

FIG. 1 shows and provides more detail of a conventional solvent mining system as described above.

The conventional solution mine create an individual caverns 100 by dissolving salt 101 from beneath the ore body 102, then rubblizing the ore into the cavern and dissolving the ore in a solution of fresh water or dilute brines 103 to form near saturated solutions at temperatures equal to ore temperature (or slightly higher). The caverns tend to develop vertically and, in some cases, consideration has been given to connecting caverns. In order to collect the ore from the solution 104, evaporation and crystallization systems are necessary at the surface.

Conventional solution mining systems have difficulty raising the mine temperature in the cavern 100 above the formation temperature, as well as obtaining fully saturated brines in the solution 104. Thus at the surface, in the conventional systems, the potash concentration and temperature is raised in evaporators. This is the most expensive part of the plant using large amounts of expensive and exotic metals. Large amounts of steam are also required in this process.

FIGS. 2 to 7A show and provide more detail of the solvent mining system according to the present invention and show particularly the dissolution of the ore in the horizontal bores which form the meanders and chambers which allow the flow to extract the ore, thus avoiding the complexities of the conventional system as described above.

Turning now to FIGS. 6 and 7, there is shown in FIG. 6 the above ground system for treating the solution brought up from the mine including the vertical wells 1 and 2 which provide the injection well 1 for returning heated brine to the production formation and the production well 2 which brings to the surface the solution including the dissolved ore.

The brine from the well is fed to the first of a series of the crystallization ECWSC units 3 which are arranged in a sequential series or row with each feeding to the next.

The remainder of the system shown in FIG. 6 is simplified in view of the advantageous use of the crystallizer units described hereinafter. The system includes a centrifuge 4 for extracting the crystals, a dryer 8, a wet scrubber 9, a series of product screens 9A for grading the product, 9B (which can be used in a possible compaction circuit) and 9C (for re-screening the product prior to loading), a granular bin 9D and a discharge to transport 9E. A water well 7 provides fresh additive water as required.

As the crystallizers are arranged to provide large crystals, the use of a compactor can be avoided thus making the downstream processing simple and effective.

The crystallizers are arranged in a series of parallel rows with the number of rows being dependent on the quantity of solution to be treated. The number of crystallizers in each row is dependent on the cooling to be applied.

The system uses heat exchange systems to take the heat from the cooling medium to be returned to the brine before the brine, after extraction of the ore, is returned to the well. This can be done by transferring the cooling medium from each crystallizer of a row to the next so that the cooling medium moves from the coolest crystallizer to the warmest and thus becomes heated as it takes the heat from the treated solution. This heat is then transferred back to the extracted brine with additional heat added from a boiler 6A to provide the required temperature.

FIGS. 7 and 7A show an externally circulated wiped surface crystallizer (ECWSC) which is a significant further development of the scraped surface crystallizers that have been used for years in the sodium sulphate industry. These crystallizers have the significant advantage of being able to cool to as low as 0 degrees, or lower when supplied with a suitable coolant. In addition they are simple to operate, inexpensive, and allow recovery of most of the heat.

The crystallizer comprises a conical drum 10 with a top feed 12. Solution to be treated in the line of crystallizers is fed into the first crystallizer at the feed supply bowl 12 from an inlet 12A and this may be of the order of 4 to 5 m3/min. The drum 10 is filled to the top to define a bath of the solution containing the crystals as they are formed. A bottom hopper discharge 13 is located at the bottom of the drum for collecting the crystals falling or settling from the bath.

A surrounding heat exchange system or jacket 14 including circulating pipes or channels 15 receives a cooling medium from a supply 11 and communicating it to a return 11A. The heat exchange system 14 is arranged to generate a cooling effect of the order of 500 to 1000 BTU/sq ft/degree F. which is significantly higher than the level of 80 which is typical for conventional systems. This allows the solution in the bath to be cooled by typically 10 C to 20 C degrees for each crystallizer of the series so as to provide a total temperature drop of the order of 40 to 50 C degrees.

A wiper system 17 includes a series of wiper blades on a shaft 18 driven by a motor 19 so that the blades wipe around the inside surface of the conical drum. This acts to stir the liquid in the bath to maintain the crystals in suspension and to transfer the cool from the cooled conical surface to the liquid through the bath.

Liquid taken from the feed bowl 12 at the top of the drum is re-circulated back downward to the top 13A of the bottom collecting hopper 13 though a pump 13B and conduit 13C. This recirculation flow, which is greater than the in-feed at the supply 12A can be of the order of 30 m3/min (dependant on actual crystalliser sizing) to maintain a gradual upward flow in the bath 10. The conical shape increases the flow rate at the bottom thus tending to lift the crystals in the liquid as a suspension with the largest crystals tending to settle due to gravity separation. The gradual separation and settling causes the material in the bottom hopper 13 to reach solids content as much as 40%. This material is then extracted at a discharge 13D at a rate matching (product produced from) the in-feed either continually or as a batch discharge system. The remaining brine overflows the feed bowl 12 through 20 to the next crystallizer in series.

Thus the liquid in each crystallizer is cooled by about 10 to 15 degrees, producing high purity potash crystals. The partially cooled brine and crystal content therein is fed so that it flows forward to the next unit, in a series of up to 5 units. Final brine temperature is typically 0 to 20 degrees C. Collected crystal passes forward through the series and finally is pumped forward to the centrifuge 4 and dryer 8. Larger installations may use several parallel lines of crystallizers.

Cool barren brine from the crystallizers is reheated in heat exchangers, using the warmed cooling media, recovered heat from the process and steam or hot water from the fuel fired boiler 6A which returns the brine to the required temperature for return through the return line 1.

Cooling medium, as low as 0 degrees C. can be supplied in winter months from an air-cooled heat exchanger, or a small brine pond. Summer operation may run at coolant temperature of 16 to 25 degrees C. using a pond or a cooling tower. Some refrigeration can be used in the summer months to lower the coolant temperature with the amount of refrigeration being selected based on cost to balance the added pumping costs of increased flow rates to the mine. The design supports the recovery of heat by the cooled mother liquor, by using it as a cooling media from the warmer crystallizers.

The design of the crystallizers uses high flow rates in the ducts or channels 15 in the cooling jacket 14 to get high heat exchange rates. High flow rate of up to 8 feet/sec is obtained by selecting the right number and rotation of wipers 17 on the mounting ring 17A which wipers move on the interior surface of the heat exchange area. With proper selection of conditions, there is no build-up of crystal in the crystallizer so that the crystal is swept to or settles at the bottom discharge hopper 13 for collection and transfer to the next crystallizer. The external circulation leg 13C maintains the crystal in suspension and incorporates the fresh feed into the suspension.

The arrangement shown herein has the potential to improve crystal growth over other crystallizer systems. The unique design of these crystallizers provides for the development of supersaturated brines in the coarsest crystal bed. This reduces or eliminates the need for compaction, if coarse crystal can be grown through the crystallization process.

A saturated brine from a properly designed and operated solution mine can be converted to a final product in a simple plant as shown. Product is recovered from the brine by cooling the brine. Conventional vacuum crystallizers can be used but are limited to cooling to about 25 degrees C. A combination of vacuum crystallizers plus suitable contact cooled crystallisers, or contact cooled crystallizers alone can be used to advantage especially in Northern climates with natural cold available through part of the year to provide cooling media as low as −4 degrees C.

The system disclosed herein provides an improved crystallization system for large scale low temperature crystallization applications. The units are simple in design providing high heat exchange through the use of specially designed cooling patterns and shear inside the vessel with wipers continually wiping the inner surface. Crystal growth is enhanced by direct contact of the supersaturated brine with the growing crystals in the bath as they are maintained suspended with gradual settling.

Turning now to FIGS. 2 to 5 there is shown the underground mining system where the solution treated in the above ground system described above is used to extract the ore. Thus, as shown in FIG. 3, where an ore body 200 or bodies has been identified at a position below ground; a series of vertical holes 201 to 205 are drilled. At the underground location of the ore body, holes 210, 211, 21 and 213 are drilled in a direction generally parallel to the ground surface within the ore body to interconnect portions of the ore body to form a series of channels extending through the body.

Each hole within the body extends through the body in a generally diagonal direction so that the path moves forwardly in the body and across the body. The paths 210 to 213 are arranged in a zigzag pattern across the body which can be curved so as to be sinusoidal in shape.

The holes 201 to 205 extend from the surface to two end portions and provide a number of feed paths to of the interconnected portions to provide a feed path to and well 201, a delivery path from the series of channels. The horizontal holes 210 to 213 are each drilled in the sinusoidal or zigzag pattern back and forth across the ore body to promote a long wavelength meander through the ore formation to be extracted. Such a zigzag sinusoidal pattern can be typically 1½ or 2½ full wavelengths per vertical hole.

The solvent is then fed through the feed path to the series of channels and back through the delivery path so as to dissolve the ore and carry the ore to the surface through the delivery channel.

The flow of the solvent in the zigzag channels forms caverns by erosion of the sides of the holes meanders 215 which etch out or erode the side walls in swirl patterns dependent on the flow of the material. This widens the holes generally in the same horizontal plane as the pre-drilled holes to sweep out the ore bed over time as the erosion continues. This is shown in FIG. 4 where the solvent swirls from side to side of the drilled holes and etches out one side and then the other at different locations along the holes depending on flow patterns.

With the use of the zigzag pattern, the meanders form in a more uniform, long wavelength pattern, there by facilitating the development of the cavern along the well bore. A direction change occurs at each well intersection. This direction change results in the formation of a large diameter cavern at each intersection point with salt deposited inside the curve.

Over time the meanders increase in size and thus erode the materials on each side of the drilled hole until the whole bed is substantially eroded and removed.

The effect of the flow through the drilled holes is shown in FIG. 5 where the original hole is eroded by swirl patterns 220 which form helicoidal flow of the solvent. The helicoidal flow causes high shear against the wall and results in rapid dissolution. The slowed flow of the solvent as the meanders increase in size over the deposited salt (halite) causes back leaching or slow dissolution of the ore and erodes halite from the front roof of the cavern. Thus the holes and flow are arranged such that caverns develop at the intersection of the holes as the flow is concentrated around the periphery of the cavern.

The combination of the intersection and meander development creates an undercut of the ore body, with a circular cross section, at the periphery and a thin zone of low flow dissolution over the salt deposit whereby slow dissolution zone extends the cavern vertically over time to dissolve out the entire ore zone.

The holes are drilled vertically to the ore layer, then horizontally through the high grade ore zone near the bottom of the selected mine zone. The holes can be 1000 to 200 meters or more in length and the forward movement of the hole in its diagonal path can be of the order of 250 meters. In this way a zigzag path of one and a half wave lengths using 3 injection wells and on production well will move forward by 3×250 or 750 meters. One such arrangement with a single feed in hole and a single return hole will therefore eventually extract the ore over an area of roughly 1000 by 750 meters.

In operation, the parameters of the temperature and flow rate are controlled so that the solvent is arranged such that the material exiting through the discharge hole is substantially saturated with the dissolved ore as it emerges through the return hole. Also the solvent is arranged such that the material exiting through the discharge hole is at a temperature at or above the rock temperature at the level of the ore body.

The solvent temperature is set by adjusting the input brine temperature.

As explained above, the material exiting through the discharge hole is processed to extract the ore by cooling the material in a crystallizer plant including a series of crystallizers, with the barren brine from the crystallizers being reheated and returned to the mine to dissolve material out of the ore body. The whole process is carried out without the need for evaporation equipment. The crystallizers are arranged for large scale low temperature crystallization.

The quantity of water is added to the heated solvent to be returned through the feed path to create the solvent needed to replace the dissolved ore (potash) in the mined area. The deposition of the salt (halite) liberated from the ore in the mined area is returned to the ground so that it never leaves the mined area. Only minimal amounts of salt ever are brought to surface. The amount of water added is that quantity required to produce enough brine to occupy the volume of potash dissolved from the mine. Water may be added back to the main hot brine feed stream but an advantage will be gained by adding the water selectively to individual feed wells to manage cavern development.

The system is used with shallow deposits with low rock temperature, mid range deposits normally not amenable to conventional solution mining methods, or deep deposits, normally accessed by convention solution mining techniques. As the process continues, as needed additional holes are drilled developing the mine field for returning the ore in solution to the surface to provide feed brine to the plant. These wells will all feed through the existing labyrinth to a single production well. Obviously at some point a parallel development using a series of new horizontal wells connected to a new production well, may be needed to increase production. All production wells will normally be located close to the plant facility.

Since various modifications can be made in my invention as herein above described, and many apparently widely different embodiments of same made within the spirit and scope of the claims without department from such spirit and scope, it is intended that all matter contained in the accompanying specification shall be interpreted as illustrative only and not in a limiting sense. 

1. A method of solution mining comprising: identifying an ore body or bodies at a position below ground; drilling at least one hole from the surface downwardly to an ore body; drilling a hole in a direction generally parallel to the ground to interconnected portions of the ore body to form a series of channels extending through the body; the holes from the surface being connected to two ends of the interconnected portions to provide a feed path to and a delivery path from the series of channels; and circulating a solvent through the feed path, the series of channels and the delivery path so as to dissolve the ore and carry the ore to the surface through the delivery channel.
 2. The method according to claim 1 wherein the holes are drilled vertically to the ore body, then horizontally through the high grade ore zone near the bottom of a selected mine zone in the ore body.
 3. The method according to claim 1 wherein the holes in the ore body and the flow therethrough are arranged such that caverns develop at the intersection of the holes as the flow is concentrated around the periphery of the cavern.
 4. The method according to claim 1 wherein the solvent is arranged such that the material exiting through the delivery path is substantially saturated with the dissolved ore.
 5. The method according to claim 1 wherein the solvent is arranged such that the material exiting through the delivery path is at a temperature at or above the rock temperature at the level of the ore body.
 6. The method according to claim 1 wherein the material exiting through the delivery path is processed to extract the ore by cooling the material in a crystallizer plant including a series of crystallizers, with the barren brine from the crystallizers being reheated and returned to the mine to dissolve material out of the ore body.
 7. The method according to claim 6 wherein the processing is carried out without evaporation equipment.
 8. The method according to claim 6 wherein the crystallizers are arranged for large scale low temperature crystallization.
 9. The method according to claim 6 wherein each crystallizer comprises a vessel with an exterior cooling system and an internal wiping system providing shear inside the vessel.
 10. The method according to claim 9 wherein a plurality to wiper blades is provided continually wiping the inner surface of the vessel so that crystal growth is enhanced by direct contact of the solvent with the growing crystal.
 11. The method according to claim 6 wherein a quantity of water is added to the heated solvent to be returned through the feed path to create the solvent needed to replace the dissolved ore in the mined area.
 12. The method according to claim 11 wherein the deposition of the salt liberated from the ore in the mined area is returned to the mined area so only minimal amounts of salt ever are brought to surface.
 13. The method according to claim 1 wherein the solvent temperature is set by adjusting the input brine temperature.
 14. The method according to claim 1 used on shallow deposits with low rock temperature.
 15. The method according to claim 1 wherein as needed additional holes from the surface are drilled developing the mine field for returning the ore in solution to the surface.
 16. The method according to claim 1 wherein the combination of the intersection and meander development creates an undercut of the ore body, with a circular cross section, at the periphery and a thin zone of low flow dissolution over the salt deposit whereby slow dissolution zone extends the cavern vertically over time to dissolve out the entire ore zone.
 17. A method of solution mining comprising: identifying an ore body or bodies at a position below ground; generating a feed path through the ore body or bodies; circulating a solvent through the feed path, the series of channels and the delivery path so as to carry the ore to the surface through the delivery channel. wherein the material exiting through the delivery path is cooled to produce product in a simplified crystallizer plant with the barren brine from the crystallisers reheated and returned to the mine to dissolve material out of the ore body; and wherein a crystallization system is provided for large scale low temperature crystallization applications where high heat exchange is provided through cooling patterns and shear inside the vessel.
 18. The method according to claim 17 wherein this eliminates the need for expensive evaporation equipment and the high operating cost associated with this equipment.
 19. The method according to claim 17 wherein the crystallizer has an external recirculation system for developing an upward flow in the bath to maintain the crystals in suspension with a series of blades for wiping the interior surface.
 20. The method according to claim 17 wherein wiper blades are provided continually wiping the inner surface so that crystal growth is enhanced by direct contact of the solvent with the growing crystals.
 21. The method according to claim 17 wherein the container of the crystallizer is conical so as to provide an increased flow rate adjacent the bottom. 